Method for synthesizing olefin functional polymers using a continuous raw material feeding mode and use of olefin functional polymers

Abstract

This application proposes a method for synthesizing olefin functional polymers using a continuous feed-in mode and the use of olefin functional polymers. This method includes the steps of: introducing low-carbon olefins into a reactor, then increasing the temperature and pressure, and once the reaction temperature and pressure are reached, adding a feed-in liquor prepared from a functional monomer, initiator, and solvent to the reactor to generate a polymerization reaction; and first performing gas-solid-liquid separation on the system where the reaction has occurred to recover the low-carbon olefins, and then performing solid-liquid separation on the excess material to obtain olefin functional polymers and liquid-phase substances. In this application, the same-chain alternating copolymerization of low-carbon gaseous olefins and functional monomers is achieved by pressurized reaction between the two, improving monomer concentration and feed-in liquor utilization by heterogeneous phase polymerization, synthesizing olefin functional polymers of different molecular weights by adjusting process parameters, and achieving high reaction efficiency; in addition, the post-processing process is simple, separation and purification are easy, the solvent and unreacted feed-in liquor can be recycled, and the conversion rate of feed-in liquor and the yield of the product can be increased.

Description

Technical Field

[0001] Cross-reference to Related Applications This application claims the priority of a Chinese patent application with the application number "202310617195.3" and the application title "Method for Synthesizing Olefin Functional Polymers in Continuous Raw Material Feeding Mode", which was filed with the China National Intellectual Property Administration on May 29, 2023, and the priority of a Chinese patent application with the application number "202310727190.6" and the application title "Use of Olefin Functional Polymers", which was filed with the China National Intellectual Property Administration on June 19, 2023, and the entire contents of which are incorporated herein by reference.

[0002] Technical Field This application belongs to the technical field of organic polymerization, and specifically relates to a method for synthesizing olefin functional polymers in continuous raw material feeding mode and the use of olefin functional polymers.

Background Art

[0003] As a functional polymer material, olefin functional polymers have wide applications in aspects such as chain extension of engineering plastics, high-performance composite materials, infiltration of nylon, ink dispersion, microencapsulation, and film formation of filtration membranes, and have attracted great attention. Due to the presence of a large number of active groups in the molecular chain of olefin functional polymers, they can react with various functional groups, such as the terminal hydroxyl group or terminal amino group of nylon products, to increase the molecular weight of nylon, improve its mechanical properties, and adjust the viscosity value of nylon; in addition, olefin functional polymers can be used in the manufacture of microcapsules and also have very good application prospects in the fields of pesticides, fragrances, and pharmaceuticals.

[0004] The raw materials for synthesizing olefin functional polymers are mainly olefins and functional monomers. Currently, available polymerization methods include emulsion polymerization, suspension polymerization, and precipitation polymerization. The former two methods both require the use of large amounts of stabilizers, which remain on the polymer particles in the form of physical or chemical adsorption, affecting their performance. On the other hand, precipitation polymerization does not require the addition of stabilizers, but in traditional precipitation polymerization systems, the concentration of the monomer being polymerized is low, resulting in low polymerization efficiency, and therefore, improvements to the polymerization method are necessary.

[0005] Depending on the type of olefin or functional monomer used as the raw material for the synthesis of olefin functional polymers, a corresponding synthesis process must be used. CN101235117A discloses a copolymerization method for styrene / maleic anhydride, in which maleic anhydride and styrene as monomers, along with an organic peroxide or azo compound as an initiator, are dissolved in a medium under nitrogen gas protection and reacted at 60-90°C for 0.25-12 hours to obtain a dispersion of polymer microspheres. CN102212166A discloses a novel copolymerization method for dicyclopentadiene and maleic anhydride, in which similarly, under nitrogen gas protection, the monomer and initiator are added to an organic medium and dissolved, and reacted at 60-90°C for 2-12 hours to obtain a self-stable dispersion of monodisperse microspheres as an alternating copolymer, and further centrifugation and drying are performed to obtain a white solid of the dicyclopentadiene / maleic anhydride alternating copolymer.

[0006] In the above patents, maleic anhydride is polymerized with an olefin as a functional monomer; however, the olefin used is usually a C4 or higher olefin, and is a liquid olefin such as a diene, cycloolefin, or isomerized olefin, but there is no mention of polymerization reactions of gaseous olefins with a C4 or lower. CN113388123A discloses a method for producing high-viscosity nylon, which involves mixing a nylon salt as a prepolymer with an olefin-maleic anhydride copolymer and carrying out a polycondensation reaction to produce high-viscosity nylon. As the olefin-maleic anhydride copolymer used in this method, an alternating copolymer of ethylene-maleic anhydride can be selected, but the process method for synthesizing the copolymer with a low-carbon olefin is not clearly described.

[0007] In summary, for the synthesis of olefin functional polymers, particularly the polymerization of low-carbon olefins (C4 or less) and functional monomers, it is necessary to select an appropriate synthesis process according to the characteristics of the raw materials. This will improve production efficiency, simplify the separation process, and reduce raw material and process costs. [Overview of the Initiative]

[0008] One objective of this invention is to provide a method for synthesizing olefin functional polymers using a continuous raw material feeding mode, which addresses the problems present in conventional technologies. This method achieves the same-chain alternating copolymerization of low-carbon gaseous olefins and functional monomers through a pressurized reaction between the two, improves monomer concentration and raw material utilization through heterogeneous phase polymerization, synthesizes olefin functional polymers of different molecular weights by adjusting process parameters, and offers high reaction efficiency; the post-reaction processing is simple, separation and purification are easy, energy consumption is saved, and costs are reduced.

[0009] To achieve the above objective, the following technical solution is used in the first aspect of this application.

[0010] This invention proposes a method for synthesizing olefin functional polymers using a continuous raw material feeding mode, and this method includes the following steps.

[0011] Step (1): After introducing the low-carbon olefin into the reactor, the temperature and pressure are increased. Once the reaction temperature and pressure are reached, the raw material solution prepared from the functional monomer, initiator, and solvent is added to the reactor in a continuous raw material feeding mode to initiate the polymerization reaction;

[0012] Step (2): For the system in which the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first to recover the low-carbon olefin, the discharged low-carbon olefin is returned to Step (1) for reuse, excess material is discharged, and then solid-liquid separation is performed to obtain a solid-phase olefin functional polymer and a liquid-phase substance.

[0013] In this invention, regarding the synthesis of olefin functional polymers, the selection of olefins and functional monomers significantly affects the performance of the polymer. Because their phase states are different, the process is relatively more difficult compared to cases where both olefins and functional monomers are liquid. Furthermore, since low-carbon gaseous olefins usually do not contain side chains, the reaction difficulty is higher than that of liquid olefins. In this invention, by reacting low-carbon gaseous olefins with liquid functional monomers, monomer concentration and reaction rate can be improved by pressurized reaction and heterogeneous phase polymerization, thereby increasing the raw material conversion rate and product yield, and enabling same-chain alternating copolymerization of gaseous olefin monomers and functional monomers. In addition, olefin functional polymers of different molecular weights can be synthesized by adjusting process parameters. After polymerization is complete, a relatively stable emulsion dispersion can be obtained directly, the post-processing process is simple, and separation and purification are easy. The method is easy to operate, the reaction conditions are mild, the raw materials can be recycled, energy consumption is saved, costs are low, and it is environmentally friendly.

[0014] In this invention, the continuous raw material feeding mode allows for real-time adjustment and control of monomer and initiator concentrations during the reaction, improving monomer concentration and raw material utilization, and enabling adjustment and control of the molecular weight of the olefin functional polymer. In addition, it allows for increased initiator concentration, reduced polymerization pressure, and shortened polymerization time, while also enabling the recovery and reuse of the solvent, offering significant advantages. In this invention, since reaction raw materials are continuously added to the reactor, the reaction in the reactor occurs continuously; however, since the reacted material is intermittently post-treated, the olefin functional polymer is not synthesized continuously.

[0015] The following are preferred technical solutions for the present application, but these are not limitations to the technical solutions proposed in this application. Rather, the technical objectives and beneficial effects of the present application can be better achieved and realized through the following technical solutions.

[0016] A preferred technical application of the present invention is that the low-carbon olefin in step (1) comprises one or at least two combinations of ethylene, propylene, butene, or butadiene, and typical and non-limiting examples of such combinations include combinations of ethylene and propylene, combinations of propylene and butene, and combinations of ethylene, propylene, and butene, wherein the butene includes isomers such as 1-butene, 2-butene, or isobutylene.

[0017] Preferably, before introducing the low-carbon olefin in step (1), the reactor is evacuated and then replaced with a protective gas, the protective gas being selected to be nitrogen gas or an inert gas.

[0018] A preferred technical solution of the present invention is that the reactor in step (1) includes one of a reaction vessel, a tubular reactor, a microchannel reactor, a fluidized bed reactor, or a boiling bed reactor.

[0019] Preferably, the tubular reactor includes one of the following: a horizontal tubular reactor, an upright tubular reactor, a coil reactor, or a U-tube reactor.

[0020] Preferably, the microchannel reactor includes a gas-liquid-solid three-phase catalytic microreactor.

[0021] In this application, the selection of reactor types is based on whether the reactor can enhance the mixing, mass transfer, and heat transfer processes during the polymerization process. For example, when a microchannel reactor is used, the efficiency of heat transfer and mass transfer is high, and the reaction conditions are precisely controlled.

[0022] A preferred technical proposal of the present invention is in which the functional monomer in step (1) comprises one or at least two combinations of maleic anhydride, maleimide, or maleic acid, and typical and non-limiting examples of such combinations include combinations of maleic anhydride and maleimide, combinations of maleimide and maleic acid, and combinations of maleic anhydride, maleimide, and maleic acid.

[0023] Preferably, the initiator in step (1) includes an azo compound and / or a peroxide compound.

[0024] Preferably, the azo compound comprises one or at least two of the following: azodiisobutyronitrile, azodiisovaleronitrile, azobisisoheptonitrile, azodicyclohexylcarbonite, or 2,2'-azobis(isobutyrate)dimethyl. Typical and non-limiting examples of such combinations include a combination of azodiisobutyronitrile and azodiisovaleronitrile, a combination of azodiisobutyronitrile and azobisisoheptonitrile, a combination of azodiisobutyronitrile, azobisisoheptonitrile, and 2,2'-azobis(isobutyrate)dimethyl, and a combination of azodiisovaleronitrile, azobisisoheptonitrile, and 2,2'-azobis(isobutyrate)dimethyl.

[0025] Preferably, the peroxide compounds are dibenzoyl peroxide, dicumyl peroxide, diisobutyryl peroxide, bis(2,4-dichlorobenzoyl) peroxide, lauroyl peroxide, t-butylperoxyneoheptanoate, t-butylperoxyneodecanoate, di-sec-butyl-peroxydicarbonate, dihexadecyl peroxydicarbonate, t-pentylperoxyneodecanoate, t-butylperoxyneovalerate, di-(4-tert-butylcyclohexyl)peroxydicarbonate, dicyclohexylperoxydicarbonate, diisopropylperoxydicarbonate, dibutylperoxydicarbonate, bis(2-ethylhexyl)peroxydicarbonate, t-butylperoxy2-ethylhexano The compounds include any one or at least two of the following: eth, ditetradecyl peroxydicarbonate, t-butyl peroxyacetate, cumyl peroxyneodecanoate, di-t-butyl peroxide, cyclohexylsulfonyl acetyl peroxide, 1,1,3,3-tetramethylbutyl peroxyneodecanoate, di(3-methoxybutyl)peroxy-dicarbonate, or 1,1,3,3-tetramethylbutyl peroxypivalate. Typical and non-limiting examples of such combinations include combinations of dibenzoyl peroxide and lauroyl peroxide, combinations of dibenzoyl peroxide and dicumyl peroxide, and combinations of lauroyl peroxide, dicumyl peroxide, and diisopropyl peroxydicarbonate.

[0026] Preferably, the solvent in step (1) comprises one or at least two combinations of an organic alkyl ester compound, an alkane compound, or an aromatic hydrocarbon compound. Typical and non-limiting examples of such combinations include combinations of an organic alkyl ester compound and an alkane compound, combinations of an alkane compound and an aromatic hydrocarbon compound, and combinations of an organic alkyl ester compound, an alkane compound, and an aromatic hydrocarbon compound.

[0027] Preferably, the general formula of the organoalkyl acid ester compound is represented by the following formula 1, [Chemical formula]

[0028] In the formula, R1 is any one of H, an alkane group having 1 to 20 carbon atoms or an aromatic hydrocarbon group having 6 to 10 carbon atoms, and R2 is any one of an alkane having 1 to 20 carbon atoms or an aromatic hydrocarbon group having 6 to 10 carbon atoms.

[0029] Preferably, the organic alkyl acid ester compound includes any one or at least a combination of two of ethyl formate, propyl formate, isobutyl formate, amyl formate, ethyl acetate, butyl acetate, isobutyl acetate, amyl acetate, isoamyl acetate, benzyl acetate, phenyl acetate, methyl propionate, ethyl propionate, propyl propionate, butyl propionate, methyl butyrate, ethyl butyrate, propyl butyrate, butyl butyrate, isobutyl butyrate, isoamyl butyrate, ethyl isobutyrate, ethyl isoamylate, isoamyl isovalerate, methyl benzoate, ethyl benzoate, propyl benzoate, butyl benzoate, isoamyl benzoate, methyl phenylacetate, ethyl phenylacetate, propyl phenylacetate, butyl phenylacetate or isoamyl phenylacetate. Typical and non-limiting examples of the combination include combinations of ethyl acetate and butyl acetate, propyl formate and ethyl acetate, combinations of ethyl acetate, ethyl propionate and ethyl butyrate, etc.

[0030] Preferably, the alkane compound includes any one or at least a combination of two of cyclohexane, n-hexane, n-heptane, n-pentane, n-octane or n-decane. Typical and non-limiting examples of the combination include combinations of cyclohexane and n-hexane, combinations of cyclohexane and n-heptane, combinations of cyclohexane, n-hexane and n-heptane, etc.

[0031] Preferably, the aromatic hydrocarbon compound comprises one or at least two of benzene, toluene, ethylbenzene, or xylene, and typical and non-limiting examples of such combinations include combinations of benzene and ethylbenzene, benzene and toluene, toluene and ethylbenzene, ethylbenzene and xylene, and benzene, ethylbenzene, and xylene.

[0032] A preferred technical solution of the present invention is one in which the molar ratio of the initiator to the functional monomer in step (1) is (0.001 to 0.2):1, such as 0.001:1, 0.005:1, 0.01:1, 0.05:1, 0.1:1, 0.15:1, or 0.2:1. However, the values ​​are not limited to those listed, and other unlisted values ​​within this range can also be applied, preferably (0.001 to 0.03):1.

[0033] Preferably, the mass ratio of the solvent to the functional monomer in step (1) is (2 to 50):1, for example, 2:1, 5:1, 10:1, 20:1, 25:1, 30:1, 35:1, 40:1 or 50:1, however, not limited to the values ​​listed, other values ​​within the range not listed may also be applied, preferably (2 to 10):1.

[0034] Preferably, impurities are removed and the mixture is preheated before adding the raw material liquid in step (1) to the reactor.

[0035] In this application, it is necessary to preheat the raw material liquid before supplying it in order to ensure that the monomers in the system are sufficiently dissolved but do not precipitate. At the same time, the preheating temperature should not be too high so as not to cause premature decomposition and consumption of the initiator. Furthermore, the components must be mixed to form the raw material liquid, and if undissolved impurities exist after mixing, these impurities must be removed by operations such as filtration.

[0036] Preferably, the raw material liquid in step (1) is pressurized by a transport pump and then pumped into the reactor at a constant rate.

[0037] In this invention, in order to ensure the continuous progress of the reaction, the raw material liquid is introduced continuously, discharged when the residence time is reached, and the subsequent separation and rectification processes are carried out after the reaction discharge step.

[0038] In the present invention, a preferred technical method is to use a polymerization reaction temperature in step (1) of 50 to 150°C, such as 50°C, 60°C, 70°C, 75°C, 80°C, 90°C, 100°C, 110°C, 120°C, or 150°C. However, the temperature is not limited to those listed above; other unlisted values ​​within this range are also applicable, preferably 70 to 120°C.

[0039] Preferably, the pressure of the polymerization reaction in step (1) is 0.1 to 10 MPa, for example, 0.1 MPa, 0.5 MPa, 1 MPa, 3 MPa, 5 MPa, 6 MPa, 8 MPa, or 10 MPa. However, it is not limited to the values ​​listed above; other values ​​within this range that are not listed may also be applied, preferably 2 to 8 MPa.

[0040] Preferably, the supply time of the raw material liquid in step (1) is 0.1 to 10 hours, for example, 0.1 hours, 0.5 hours, 1 hour, 2 hours, 3 hours, 4 hours, 5 hours, 6 hours, 8 hours, or 10 hours. However, the values ​​are not limited to those listed, and other values ​​within that range that are not listed may also be applied.

[0041] Preferably, the residence time of the raw material liquid in step (1) is 0.1 to 15 hours, for example, 0.1 hours, 0.5 hours, 1 hour, 3 hours, 5 hours, 6 hours, 8 hours, 10 hours, 12 hours, or 15 hours. However, the values ​​are not limited to those listed above, and other values ​​within that range that are not listed may also be applied.

[0042] Preferably, during the polymerization reaction process in step (1), a low-carbon olefin is continuously introduced to maintain the pressure.

[0043] A preferred technical solution of the present invention involves discharging and recovering the low-carbon olefin during the gas-solid-liquid separation process in step (2), and replacing it with a protective gas, wherein nitrogen gas or an inert gas is selected as the protective gas.

[0044] Preferably, the excess material from which the low-carbon olefin is recovered in step (2) is discharged in solid-liquid form.

[0045] Preferably, the discharged low-carbon olefin is pressurized and then returned to step (1) for reuse, and the pressure after pressurization is selected within the range of reaction pressures described above.

[0046] A preferred technical solution of the present invention is a method for solid-liquid separation in step (2) which includes one or at least two of the following: decantation, filtration, or centrifugation, and typical and non-limiting examples of such combinations include a combination of decantation and filtration, a combination of filtration and centrifugation, and a combination of decantation, filtration, and centrifugation.

[0047] Preferably, the filtration includes one of gravity filtration, vacuum filtration, or pressure filtration.

[0048] Preferably, the filter used for filtration includes an atmospheric pressure filter, a vacuum filter, or a pressurized filter.

[0049] Preferably, the excess material is subjected to pressure filtration with a protective gas, and the resulting filtration cake is washed, dried, and then crushed.

[0050] Preferably, the washing is carried out using the solvent in step (1), and may also be carried out using an ether compound, the ether compound comprising any one or at least two combinations of C1 to C10 saturated ether compounds, preferably ethyl ether and / or propyl ether.

[0051] Preferably, the drying temperature is 30 to 150°C, for example, 30°C, 40°C, 50°C, 60°C, 70°C, 80°C, 90°C, 100°C, 110°C, or 120°C. However, it is not limited to the values ​​listed above; other values ​​within this range that are not listed may also be applied, preferably 80 to 120°C.

[0052] Preferably, the drying time is 1 to 72 hours, for example, 1 hour, 6 hours, 12 hours, 18 hours, 24 hours, 30 hours, 36 hours, 42 hours, 48 ​​hours, 54 hours, 60 hours, 66 hours, or 72 hours. However, the drying time is not limited to the listed values, and other values ​​within the range that are not listed may also be applied, preferably between 24 and 72 hours.

[0053] Preferably, the drying pressure is 0.1 to 101 kPa, such as 0.1 kPa, 1 kPa, 10 kPa, 20 kPa, 40 kPa, 60 kPa, 80 kPa, or 101 kPa. However, it is not limited to the values ​​listed above; other values ​​within this range that are not listed may also be applied, preferably between 1 and 10 kPa.

[0054] Preferably, the olefin functional polymer in step (2) is a microspherical particle with a particle size of 10 to 50 μm, such as 10 μm, 15 μm, 20 μm, 25 μm, 30 μm, 35 μm, 40 μm, or 50 μm, however, it is not limited to the values ​​listed above, and other values ​​within that range that are not listed may also be applied.

[0055] A preferred technical solution of this invention is to separate the liquid phase substance in step (2) and return the recovered solvent to step (1) for reuse.

[0056] In this invention, the liquid phase substance can be recovered and reused without separation, and can be used in the preparation of raw material liquids or as a washing solvent.

[0057] Preferably, the method for separating the liquid phase substance in step (3) includes one or at least two combinations of distillation, membrane separation, washing, or extraction, with typical and non-limiting examples of such combinations including a combination of distillation and membrane separation, a combination of distillation and extraction, a combination of distillation, membrane separation, and washing, and preferably distillation.

[0058] Preferably, the recovered solvent is returned to step (1) and / or step (2) for reuse and used for preparing the raw material liquid and / or washing the filtered cake.

[0059] A preferred technical proposal of this application includes the following steps:

[0060] Step (1): After introducing a low-carbon olefin into the reactor, the temperature and pressure are increased, wherein the low-carbon olefin includes one or at least two of ethylene, propylene, butene, or butadiene, and the reactor includes one of a reactor vessel, a tubular reactor, a microchannel reactor, a fluidized bed reactor, or a boiling bed reactor; once the reaction temperature and pressure are reached, a feedstock solution prepared from a functional monomer, an initiator, and a solvent is added to the reactor in a continuous feedstock mode, wherein the functional monomer includes one or at least two of maleic anhydride, maleimide, or maleic acid, and the initiator is an azo compound and / or The solvent contains a peroxide compound, and the solvent comprises one or at least two of the following: an organic alkyl ester compound, an alkane compound, or an aromatic hydrocarbon compound; the molar ratio of the initiator to the functional monomer is (0.001~0.2):1; and the mass ratio of the solvent to the functional monomer is (2~50):1; the raw material liquid is pressurized by a transfer pump and then pumped into the reactor to generate a polymerization reaction, wherein the polymerization reaction temperature is 50~150°C, the pressure is 0.1~10 MPa, the supply time is 0.1~10 h, and the residence time is 0.1~15 h; low-carbon olefins are continuously introduced during the polymerization reaction to maintain the pressure;

[0061] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first. During the gas-solid-liquid separation process, excess low-carbon olefin is discharged and replaced with a protective gas. The discharged low-carbon olefin is pressurized and returned to Step (1) for reuse. The excess material is discharged in solid-liquid form and solid-liquid separation is performed. The excess material is pressure-filtered with a protective gas, and the resulting filtration cake is washed, dried, and then crushed. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained. However, the olefin functional polymer is in the form of microspherical particles with a particle size of 10 to 50 μm.

[0062] Step (3): The liquid phase substance obtained in step (2) is separated, and the separation method includes one or at least two of the following: distillation, membrane separation, washing, or extraction; the recovered solvent is returned to step (1) and / or step (2) for reuse and used for preparing the raw material liquid and washing the filtration cake.

[0063] Compared to conventional technology, this invention can provide the following beneficial effects.

[0064] (1) The method described in this application employs a heterogeneous phase polymerization method, achieving co-chain alternating copolymerization of a low-carbon gaseous olefin and a liquid functional monomer through a pressurized reaction, thereby enabling the production of olefin functional polymers with high functional group content, high reaction activity, and wide applicability; (2) In this invention, a relatively stable emulsion dispersion can be obtained directly after polymerization is complete, the post-processing process is simple, separation and purification are easy, the raw materials can be recycled, and the conversion rate of the raw materials and the yield of the product are high; (3) The method described herein allows for the real-time adjustment and control of monomer and initiator concentrations during the reaction by continuously supplying the raw material liquid, thereby improving monomer concentration and raw material utilization, and adjusting and controlling the molecular weight of the olefin functional polymer. In addition, it is possible to increase the initiator concentration, lower the polymerization pressure, and shorten the total process flow time. (4) The method described herein makes it possible to completely close the reaction system equipment and prevent airborne impurities from entering the reaction system during the low-carbon olefin circulation process; (5) The method described in the present invention is easy to operate, requires mild reaction conditions, saves energy, is low-cost, and is environmentally friendly.

[0065] A second aspect of this application proposes the use of the olefin functional polymer according to the first aspect described above, and such use includes the use of the olefin functional polymer in the manufacture of a modified reinforced resin, an adhesive, a scale inhibitor, or a glass fiber wetting agent. However, the use of the olefin functional polymer in the manufacture of a reinforced resin includes the step of mixing the olefin functional polymer with a matrix resin and a filler to obtain a modified reinforced resin; the use of the olefin functional polymer in the manufacture of a modified adhesive includes the step of causing an esterification reaction between the olefin functional polymer and alcohols to obtain an adhesive; the use of the olefin functional polymer in the manufacture of a scale inhibitor includes the step of performing an anionization reaction on the olefin functional polymer to obtain a scale inhibitor; and the use of the olefin functional polymer in the manufacture of a glass fiber wetting agent includes the step of mixing the olefin functional polymer with a coupling agent, a pH adjuster, and water to obtain a glass fiber wetting agent.

[0066] In this invention, the selection of olefins and functional monomers significantly affects the performance of olefin functional polymers. In this invention, a low-carbon gaseous olefin is reacted with a liquid functional monomer. Because the phase states of the two are different, the reaction is relatively more difficult compared to cases where both the olefin and functional monomer are liquid. Furthermore, since low-carbon gaseous olefins usually do not contain side chains, the reaction difficulty is higher than that of liquid olefins. In this invention, monomer concentration and reaction rate can be improved by pressurized reaction and heterogeneous phase polymerization, increasing the raw material conversion rate and product yield, and enabling same-chain alternating copolymerization of gaseous olefin monomers and functional monomers. In this invention, the operating process is simple, the reaction conditions are mild, separation and purification are easy, raw materials can be recycled, energy consumption is saved, costs are low, and it is environmentally friendly.

[0067] At the same time, this invention utilizes the high content of functional groups and high reactivity of olefin functional polymers to produce various modified materials suitable for different domains by using olefin functional polymers as a reaction platform and utilizing their derivatization pathway to perform chemical reactions such as esterification, hydrolysis, and modification. This enables the development of various downstream products such as compatible modifiers, adhesives, and scale inhibitors, thereby expanding the application range of olefin functional polymers.

[0068] (A) Use of olefin functional polymers in the manufacture of reinforced resins A preferred technical method of this application involves mixing the olefin functional polymer according to the first embodiment described above with a matrix resin and a filler as a compatibility modifier.

[0069] Preferably, the matrix resin includes thermoplastics and / or thermosetting plastics.

[0070] Preferably, the thermoplastic includes one or at least two combinations of PC, PA, POM, PBT, PET, PVC, PS, PE, or ABS, and typical and non-limiting examples of such combinations include combinations of PC and PA, PA and PET, PET, PVC and PS, and PC, PBT, PVC and ABS.

[0071] Preferably, the thermosetting plastic comprises one or at least two of EP, UPR, PU, ​​or UF, and typical and non-limiting examples of such combinations include combinations of EP and UPR, combinations of UPR and PU, and combinations of EP, PU, ​​and UF.

[0072] Preferably, the filler includes inorganic fillers and / or organic fillers.

[0073] Preferably, the amount of matrix resin added accounts for 30 to 90 wt% of the total amount of the mixture, for example, 30 wt%, 40 wt%, 50 wt%, 60 wt%, 70 wt%, 80 wt%, or 90 wt%, however, other unlisted values ​​within that range are also applicable; the amount of filler added accounts for 5 to 65 wt% of the total amount of the mixture, for example, 5 wt%, 10 wt%, 20 wt%, 30 wt%, or 40 wt%. Examples include %, 50 wt%, 60 wt%, or 65 wt%, however, other unlisted values ​​within that range are also applicable, not limited to the listed values; the amount of olefin functional polymer added accounts for 3 to 15 wt% of the total amount of the mixture, for example, 3 wt%, 5 wt%, 8 wt%, 10 wt%, 12 wt%, or 15 wt%, however, other unlisted values ​​within that range are also applicable, not limited to the listed values.

[0074] A preferred technical application of the present invention is a mixing method comprising one of a mechanical blend, a solution blend, or a latex blend.

[0075] Preferably, the mechanical blend includes pre-mixing an olefin functional polymer with a matrix resin and a filler, followed by kneading and mixing, and then extrusion granulation to produce a modified and reinforced resin.

[0076] Preferably, the kneading and mixing are performed in a kneader, and the temperature of the kneading and mixing is 120 to 400°C, such as 120°C, 150°C, 180°C, 200°C, 250°C, 300°C, 350°C, or 400°C. However, the temperature is not limited to the values ​​listed above, and other values ​​within that range that are not listed may also be applied.

[0077] Preferably, the extrusion granulation is carried out using a twin-screw extruder or a single-screw extruder.

[0078] Preferably, the solution blend comprises dissolving an olefin functional polymer, a matrix resin, and a filler in a solvent, uniformly mixing them, and then removing the solvent to obtain a modified and reinforced resin.

[0079] Preferably, the solvent comprises one or at least two combinations of an organic alkyl ester compound, an alkane compound, or an aromatic hydrocarbon compound. Typical and non-limiting examples of such combinations include combinations of an organic alkyl ester compound and an alkane compound, combinations of an alkane compound and an aromatic hydrocarbon compound, and combinations of an organic alkyl ester compound, an alkane compound, and an aromatic hydrocarbon compound.

[0080] Preferably, the method for removing the solvent is pressurized filtration.

[0081] Preferably, the latex blend includes dissolving an olefin functional polymer, a matrix resin, and a filler in a solvent, then producing latex by distillation, and obtaining a modified and reinforced resin by uniformly mixing, followed by aggregation, drying, and plasticization.

[0082] (B) Use of olefin functional polymers in the manufacture of adhesives A preferred technical application of the present invention includes a combination of one or at least two of methanol, ethanol, propanol, or butanol, and typical and non-limiting examples of such combinations include a combination of methanol and ethanol, a combination of ethanol and butanol, and a combination of methanol, ethanol, and butanol.

[0083] Preferably, the molar ratio of acid anhydride to alcohols in the olefin functional polymer is 1:(2~5), for example, 1:2, 1:2.5, 1:3, 1:3.5, 1:4, 1:4.5, or 1:5. However, other values ​​within this range that are not listed may also be applied.

[0084] Preferably, the temperature of the esterification reaction is 60 to 80°C, such as 60°C, 65°C, 70°C, 75°C, or 80°C. However, the temperature is not limited to the values ​​listed above; other values ​​within this range that are not listed may also be used.

[0085] Preferably, the duration of the esterification reaction is 3 to 5 hours, for example, 3 hours, 3.5 hours, 4 hours, 4.5 hours, or 5 hours. However, the duration is not limited to the values ​​listed above; other values ​​within this range that are not listed may also be applied.

[0086] Preferably, after the esterification reaction, the product is concentrated and dried to obtain the esterification product.

[0087] A preferred technical method of the present invention further includes generating a monoesterified olefin functional polymer by causing an esterification reaction between the olefin functional polymer and alcohols prior to the anionization reaction.

[0088] Preferably, the alcohols include one or at least two of methanol, ethanol, butanol, ethylene glycol, or propylene glycol, and typical and non-limiting examples of such combinations include methanol and ethanol, ethanol and ethylene glycol, methanol, ethanol and butanol, and ethanol, ethylene glycol and propylene glycol.

[0089] Preferably, the molar ratio of acid anhydride to alcohol in the olefin functional polymer is 1:(1~10), such as 1:1, 1:2, 1:3, 1:4, 1:5, 1:6, 1:8, or 1:10. However, other values ​​within this range that are not listed may also be applied.

[0090] Preferably, the temperature of the esterification reaction is 50 to 80°C, such as 50°C, 55°C, 60°C, 65°C, 70°C, 75°C, or 80°C. However, the temperature is not limited to the values ​​listed above; other values ​​within this range that are not listed may also be used.

[0091] Preferably, the pressure for the esterification reaction is 0 to 0.5 MPa, such as 0 MPa, 0.1 MPa, 0.2 MPa, 0.3 MPa, 0.4 MPa, or 0.5 MPa. However, other values ​​within this range that are not listed may also be applied.

[0092] Preferably, the duration of the esterification reaction is 0.5 to 24 hours, for example, 0.5 hours, 1 hour, 2 hours, 4 hours, 6 hours, 8 hours, 12 hours, 16 hours, 20 hours, or 24 hours. However, the duration is not limited to the values ​​listed above; other values ​​within this range that are not listed may also be applied.

[0093] (C) Use of Olefin Functional Polymers in the Manufacture of Scale Inhibitors Preferably, the anionization reaction includes the reaction of an olefin functional polymer or a monoesterified olefin functional polymer with a quaternary ammonium salt, an alkali, or an acid.

[0094] Preferably, the quaternary ammonium salt comprises one or at least two of the following: epoxypropyltrimethylammonium chloride, octadecyldimethylammonium chloride, octadecylamine polyoxyethylene ether bisquaternary ammonium salt, or bisdodecylamine polyoxyethylene ether monoquaternary ammonium salt. Typical and non-limiting examples of such combinations include combinations of epoxypropyltrimethylammonium chloride and octadecyldimethylammonium chloride, combinations of octadecyldimethylammonium chloride and octadecylamine polyoxyethylene ether bisquaternary ammonium salt, and combinations of epoxypropyltrimethylammonium chloride, octadecyldimethylammonium chloride, and bisdodecylamine polyoxyethylene ether monoquaternary ammonium salt.

[0095] Preferably, the alkali includes a caustic alkali added in the form of an alkaline solution.

[0096] Preferably, when using the quaternary ammonium salt, an alkaline solution is added at the same time.

[0097] Preferably, the acid comprises one or at least two of sulfuric acid, persulfuric acid, or phosphorus pentoxide, and typical and non-limiting examples of such combinations include a combination of sulfuric acid and persulfuric acid, a combination of persulfuric acid and phosphorus pentoxide, or a combination of sulfuric acid, persulfuric acid, and phosphorus pentoxide.

[0098] Preferably, the anionization reaction includes one or at least two of the following: reacting a monoesterified olefin functional polymer with a quaternary ammonium salt in an alkaline solution to produce a cationic polymer scale inhibitor; reacting an olefin functional polymer with a quaternary ammonium salt in an alkaline solution to produce a cationic polymer scale inhibitor; generating a saponification reaction between an olefin functional polymer and an alkaline solution to produce a carboxylate-type anionic polymer scale inhibitor; reacting a diol-based monoesterified olefin functional polymer with sulfuric acid to produce a sulfate-ester-type anionic polymer scale inhibitor; or reacting a diol-based monoesterified olefin functional polymer with phosphorus pentoxide to produce a phosphate-type anionic polymer scale inhibitor.

[0099] (D) Use of olefin functional polymers in the manufacture of glass fiber wetting agents A preferred technical solution of the present invention includes a combination of one or at least two of the following: a silane coupling agent, an aluminate ester coupling agent, or a titanate ester coupling agent. Typical and non-limiting examples of such combinations include a combination of a silane coupling agent and an aluminate ester coupling agent, a combination of a silane coupling agent and a titanate ester coupling agent, and a combination of a silane coupling agent, an aluminate ester coupling agent, and a titanate ester coupling agent.

[0100] In this application, among the coupling agents mentioned above, the most widely used are silane coupling agents, and the selectable types include A-151 (vinyltriethoxysilane), KH550 (γ-aminopropyltriethoxysilane), KH570 (γ-methacryloyloxypropyltrimethoxysilane), and currently, novel silane coupling agents such as organosilicon peroxide coupling agents are also used.

[0101] Preferably, the pH adjusting agent includes an acid adjusting agent or an alkali adjusting agent.

[0102] Preferably, the acidity regulator comprises one or at least two of acetic acid, citric acid, formic acid, or oxalic acid, and typical and non-limiting examples of such combinations include a combination of formic acid and acetic acid, a combination of citric acid and oxalic acid, and a combination of acetic acid, citric acid, and formic acid.

[0103] Preferably, the alkalinity adjusting agent comprises one or at least two of the following: aqueous ammonia, sodium hydroxide, sodium bicarbonate, alkaline amino acids, or organic amine systems. Typical and non-limiting examples of such combinations include combinations of aqueous ammonia and sodium hydroxide, sodium hydroxide and sodium bicarbonate, aqueous ammonia and organic amine systems, and combinations of sodium bicarbonate, alkaline amino acids, and organic amine systems.

[0104] Preferably, the manufacturing process of the glass fiber wetting agent includes adding a coupling agent to water and stirring, then adding a solid-phase olefin functional polymer, stirring uniformly, and then adding a pH adjusting agent to obtain the glass fiber wetting agent.

[0105] Preferably, after adding the coupling agent, the stirring time is 20 to 30 minutes, for example, 20 minutes, 22 minutes, 25 minutes, 27 minutes, or 30 minutes. However, other values ​​within this range that are not listed may also be applied.

[0106] Preferably, after adding the olefin functional polymer, the stirring time is 60 to 240 min, for example 60 min, 90 min, 120 min, 150 min, 180 min, 210 min, or 240 min, however, not limited to the values ​​listed, other values ​​within this range that are not listed may also be applied; the stirring speed is 100 to 800 rpm, for example 100 rpm, 200 rpm, 300 rpm, 400 rpm, 500 rpm, 600 rpm, 700 rpm, or 800 rpm, however, not limited to the values ​​listed, other values ​​within this range that are not listed may also be applied.

[0107] Preferably, after adding a pH adjusting agent, the pH value is adjusted to 6-10, for example, 6, 7, 8, 9, or 10. However, other unlisted values ​​within this range are also applicable, not limited to the values ​​listed above.

[0108] Preferably, in the glass fiber wetting agent, the mass percentage of water is 20 to 95 wt%, such as 20 wt%, 30 wt%, 40 wt%, 50 wt%, 60 wt%, 70 wt%, 80 wt%, 90 wt%, or 95 wt%, however, other values ​​within this range that are not listed may also be applied, and the remainder is a solid phase component.

[0109] A preferred technical solution of the present invention is one in which the glass fiber wetting agent in step (3) further comprises a combination of one or at least two of the following: a lubricant, an antifoamer, or an antioxidant. Typical and non-limiting examples of such combinations include a combination of a lubricant and an antifoamer, a combination of an antifoamer and an antioxidant, and a combination of a lubricant, an antifoamer, and an antioxidant.

[0110] Preferably, the lubricant comprises one or at least two of the following: stearic acid amide, oleic acid amide, palmitic acid amide, stearic acid, methyl stearate, butyl stearate, polyethylene wax, or polypropylene wax. Typical and non-limiting examples of such combinations include a combination of stearic acid amide and oleic acid amide, a combination of stearic acid and methyl stearate, a combination of polyethylene wax and polypropylene wax, and a combination of oleic acid amide, palmitic acid amide, and stearic acid.

[0111] Preferably, the defoaming agent comprises a combination of one or at least two of the following: a high-carbon alcohol fatty acid ester complex, polyoxyethylene polyoxypropylene pentaerythritol ether, polyoxyethylene polyoxypropyl alcohol amine ether, polyoxypropylene glyceryl ether, or polyoxypropylene. Typical and non-limiting examples of such combinations include a combination of a high-carbon alcohol fatty acid ester complex and polyoxyethylene polyoxypropylene pentaerythritol ether, a combination of polyoxyethylene polyoxypropyl alcohol amine ether and polyoxypropylene glyceryl ether, and a combination of polyoxyethylene polyoxypropylene pentaerythritol ether, polyoxyethylene polyoxypropyl alcohol amine ether, and polyoxypropylene glyceryl ether.

[0112] Preferably, the antioxidant includes a hindered phenol antioxidant and / or a phosphite ester antioxidant.

[0113] Preferably, the antioxidants are antioxidant 1010 (tetra[β-(3.5-di-tert-butyl-4-hydroxyphenyl)propanoic acid]pentaerythritol ester), antioxidant 1076 (β-(3.5-di-tert-butyl-4-hydroxyphenyl)propionic acid octadecanol ester), antioxidant 3114 (1,3,5-tri(3,5-di-tert-butyl-4-hydroxybenzyl)isocyanuric acid), antioxidant 168 (tri[2. The product comprises one or at least two combinations of either 4-di-tert-butylphenyl]phosphite or antioxidant 626 (bis(2,4-di-tert-butylphenyl)pentaerythritol diphosphite), typical and non-limiting examples of such combinations include the combination of antioxidant 1010 and antioxidant 1076, the combination of antioxidant 168 and antioxidant 626, and the combination of antioxidant 3114 and antioxidant 168.

[0114] Preferably, the lubricant, defoamer, and antioxidant are added simultaneously with the olefin functional polymer during the production of the glass fiber wetting agent.

[0115] In this application, when producing a glass fiber wetting agent using an olefin functional polymer, copolymer monomers may be added when synthesizing the olefin functional polymer required. The result is a multi-component olefin functional polymer, which can effectively adjust the anhydride value of the olefin functional polymer. However, the type of copolymer monomer includes one or at least two combinations of methyl acrylate, methyl methacrylate, vinyl acetate, N,N-dimethylacrylamide, acrylamide, or acrylonitrile. Typical and non-limiting examples of such combinations include combinations of methyl acrylate and methyl methacrylate, methyl acrylate and vinyl acetate, N,N-dimethylacrylamide, acrylamide, and acrylonitrile, and methyl methacrylate, vinyl acetate, and acrylamide.

[0116] A preferred technical application of this invention includes the following steps:

[0117] Step (1): After introducing a low-carbon olefin into the reactor, the temperature and pressure are increased, wherein the low-carbon olefin includes one or at least two of ethylene, propylene, butene, or butadiene, and the reactor includes one of a kettle reactor, a tubular reactor, a microchannel reactor, a column reactor, a fluidized bed reactor, or a boiling bed reactor; once the reaction temperature and pressure are reached, a stock solution prepared from a functional monomer, an initiator, and a solvent is added to the reactor, wherein the functional monomer includes one or at least two of maleic anhydride, maleimide, or maleic acid, and the initiator is an azo compound and / or a peroxide compound, wherein the solvent comprises one or at least two combinations of an organic alkyl ester compound, an alkane compound, or an aromatic hydrocarbon compound, the molar ratio of the initiator to the functional monomer is (0.001~0.2):1, and the mass ratio of the solvent to the functional monomer is (2~50):1; the raw material liquid is pressurized by a transfer pump and then pumped at a constant rate into the reactor to generate a polymerization reaction, wherein the polymerization reaction temperature is 50~150°C, the pressure is 0.1~10 MPa, and the residence time is 10 s~10 h; low-carbon olefins are continuously introduced during the polymerization reaction to maintain the pressure;

[0118] Step (2): The material from which the polymerization reaction in Step (1) has occurred is first subjected to gas-solid-liquid separation to recover the low-carbon olefin, the discharged low-carbon olefin is pressurized and returned to Step (1) for reuse, the excess material is discharged in solid-liquid form and subjected to solid-liquid separation, pressure-filtered with a protective gas, and the resulting filtration cake is dried to obtain a solid-phase olefin functional polymer and a liquid-phase substance, wherein the olefin functional polymer is in the form of microspherical particles with a particle size of 10 to 50 μm; separation is performed on the liquid-phase substance, wherein the separation method includes one or at least two of the following: distillation, membrane separation, washing, or extraction; the separated recovered solvent is returned to Step (1) and / or Step (2) for reuse and used for preparing the raw material liquid and washing the filtration cake;

[0119] Step (3): The olefin functional polymer obtained in Step (2) is mixed with a matrix resin and a filler as a compatibility modifier, wherein the matrix resin includes thermoplastics and / or thermosetting plastics, the filler includes inorganic fillers and / or organic fillers, the amount of matrix resin added accounts for 30-90 wt% of the total mixture, the amount of filler added accounts for 5-65 wt% of the total mixture, and the amount of olefin functional polymer added accounts for 3-15 wt% of the total mixture; the mixing method includes one of mechanical blending, solution blending, or latex blending; thus a modified and strengthened resin is obtained;

[0120] Step (2) is used to induce an esterification reaction between the olefin functional polymer and alcohols, wherein the alcohols include one or at least two of methanol, ethanol, propanol, or butanol, the molar ratio of acid anhydride to alcohols in the olefin functional polymer is 1:(2~5), the temperature of the esterification reaction is 60~80°C, the time is 3~5h, and further concentration and drying are performed to obtain the adhesive;

[0121] Step (2) involves performing an anionization reaction on the olefin functional polymer to obtain a scale inhibitor; further comprising, prior to the anionization reaction, generating a monoesterified olefin functional polymer by causing an esterification reaction between the olefin functional polymer and alcohols, wherein the alcohols include one or at least two of methanol, ethanol, butanol, ethylene glycol, or propylene glycol; and the anionization reaction includes the reaction of the olefin functional polymer or monoesterified olefin functional polymer with a quaternary ammonium salt, alkali, or acid, wherein the quaternary ammonium salt is epoxypropyltrimethylammonium chloride, octadecyldimethylammonium chloride, octadecylamine polyoxyethylene ether bisquaternary ammonium salt, or bisdodecylamine polyoxyethylene ether monoquaternary ammonium The reaction comprises one or at least two combinations of nium salts; the anionic / cationic reaction comprises one or at least two combinations of the following: reacting a monoesterified olefin functional polymer with a quaternary ammonium salt in an alkaline solution to produce a cationic polymer scale inhibitor; reacting an olefin functional polymer with a quaternary ammonium salt in an alkaline solution to produce a cationic polymer scale inhibitor; causing a saponification reaction between an olefin functional polymer and an alkaline solution to produce a carboxylate-type anionic polymer scale inhibitor; reacting a diol-based monoesterified olefin functional polymer with sulfuric acid to produce a sulfate-ester-type anionic polymer scale inhibitor; or reacting a diol-based monoesterified olefin functional polymer with phosphorus pentoxide to produce a phosphate-type anionic polymer scale inhibitor;

[0122] Alternatively, the olefin functional polymer prepared in step (2) is mixed with a coupling agent, a pH adjuster, and water. Specifically, the coupling agent is added to the water and stirred for 20-30 minutes, then the lubricant, olefin functional polymer, defoamer, and antioxidant are added and stirred for 60-240 minutes, with a stirring speed of 100-800 rpm. After that, the pH adjuster is added to adjust the pH to 6-10, thereby obtaining a glass fiber wetting agent.

[0123] Compared to conventional technology, this invention offers the following beneficial effects.

[0124] (1) In this invention, a heterogeneous phase polymerization method is employed by pressurizing the reaction of a low-carbon gaseous olefin and a liquid functional monomer, and by combining this with a process of continuously supplying the raw material liquid, the low-carbon gaseous olefin and the functional monomer undergo same-chain alternating copolymerization, resulting in a molecular weight that can be controlled, has a high functional group content, high reaction activity, and can be widely used as an olefin functional polymer;

[0125] (2) In this invention, the operating process is simple, the reaction conditions are mild, separation and purification are easy, the raw materials can be recycled, energy consumption is saved, costs are low, and economic benefits are high.

[0126] (3) In this invention, by utilizing the high content of functional groups and high reaction activity in olefin functional polymers, various modified materials suitable for different fields can be manufactured by using olefin functional polymers as a reaction platform and chemical reactions such as esterification, hydrolysis, and modification, thereby developing various downstream products and expanding the range of applications of olefin functional polymers. [Brief explanation of the drawing]

[0127] [Figure 1] This is a process flowchart of the method for synthesizing olefin functional polymers using a continuous raw material feeding mode according to Example 1 of the present application. [Modes for carrying out the invention]

[0128] To better explain this application and to facilitate understanding of its proposed technology, the application will be described in more detail below. However, the following embodiments are merely simplified examples of the application and do not represent or limit the scope of protection of this application; the scope of protection of this application is governed by the claims.

[0129] (1) Method for synthesizing olefin functional polymers using a continuous raw material feeding mode In a part of the present invention for carrying out the invention, a method for synthesizing an olefin functional polymer by a continuous raw material feeding mode is provided, the method comprising the following steps.

[0130] (1) After introducing the low-carbon olefin into the reactor, the temperature and pressure are increased until the reaction temperature and pressure are reached, at which point the raw material solution prepared from the functional monomer, initiator and solvent is added to the reactor to initiate the polymerization reaction;

[0131] (2) For the system in which the polymerization reaction in step (1) has occurred, gas-solid-liquid separation is performed first to recover the low-carbon olefin, the discharged low-carbon olefin is returned to step (1) for reuse, excess material is discharged, and then solid-liquid separation is performed to obtain a solid-phase olefin functional polymer and a liquid-phase substance.

[0132] The following are typical and non-limiting embodiments of the present invention.

[0133] Example I-1 In this example, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed. The process flowchart of this method is shown in Figure 1 and includes the following steps.

[0134] Step (1): After introducing a low-carbon olefin into a microchannel reactor, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, an initiator, and a solvent is pumped into the reactor in a continuous raw material feeding mode, provided that the functional monomer is maleic anhydride, the initiator is dibenzoyl peroxide, the solvent is isoamyl acetate, the molar ratio of the initiator to the functional monomer is 0.01:1, and the mass ratio of the solvent to the functional monomer is 5:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reactor to generate a polymerization reaction, provided that the polymerization reaction temperature is 100°C, the pressure is 6 MPa, the supply time is 0.1 h, and the total residence time is 0.1 h; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0135] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is subjected to pressurized nitrogen gas filtration using a 3-in-1 filter. The resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is n-hexane, the drying temperature is 30°C, the drying time is 10 h, and the pressure is 101 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0136] Step (3): The liquid phase substance from step (2) is separated by rectification. The top fraction after rectification is returned to steps (1) and (2) respectively as the solvent for each component and reused for preparing the raw material liquid and washing the filtration cake.

[0137] Example I-2 In this example, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0138] Step (1): After introducing a low-carbon olefin into the reaction vessel, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, an initiator, and a solvent is pumped into the reaction vessel in a continuous raw material feeding mode, provided that the functional monomer is maleic anhydride, the initiator is azodiisobutyronitrile, the solvent is ethyl acetate and butyl acetate in a volume ratio of 1:1, the molar ratio of the initiator to the functional monomer is 0.1:1, and the mass ratio of the solvent to the functional monomer is 20:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reaction vessel to initiate a polymerization reaction, provided that the polymerization reaction temperature is 70°C, the pressure is 4 MPa, the supply time is 8 hours, and the total residence time is 10 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0139] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is subjected to pressurized nitrogen gas filtration using a 3-in-1 filter. The resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is butyl acetate, the drying temperature is 120°C, the drying time is 48 hours, and the pressure is 50 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0140] Step (3): The liquid phase substance from step (2) is separated by rectification. The top fraction after rectification is returned to steps (1) and (2) respectively as the solvent for each component and reused for preparing the raw material liquid and washing the filtration cake.

[0141] Example I-3 In this embodiment, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0142] Step (1): After introducing a low-carbon olefin into the reaction vessel, the temperature and pressure are increased, provided that the low-carbon olefin is isobutylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, an initiator, and a solvent is pumped into the reaction vessel in a continuous raw material feeding mode, provided that the functional monomer is maleic anhydride, the initiator is azobisisoheptonitrile, the solvent is ethyl acetate, the molar ratio of the initiator to the functional monomer is 0.06:1, and the mass ratio of the solvent to the functional monomer is 8:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reaction vessel to initiate a polymerization reaction, provided that the polymerization reaction temperature is 90°C, the pressure is 3.5 MPa, the supply time is 5 hours, and the total residence time is 7 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0143] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is subjected to pressurized nitrogen gas filtration using a 3-in-1 filter. The resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is ethyl acetate, the drying temperature is 60°C, the drying time is 24 hours, and the pressure is 20 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0144] Step (3): The liquid phase substance obtained in step (2) is subjected to rectification separation. The top fraction after rectification is returned to step (1) as a recovered solvent and reused for the preparation of the raw material liquid.

[0145] Example I-4 In this embodiment, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0146] Step (1): After introducing a low-carbon olefin into a fluidized bed reactor, the temperature and pressure are increased, provided that the low-carbon olefin is propylene; before introducing the low-carbon olefin, argon gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, an initiator, and a solvent is pumped into the fluidized bed reactor in a continuous raw material feeding mode, provided that the functional monomer is maleimide, the initiator is dicumyl peroxide, the solvent is benzene and xylene in a volume ratio of 1:1, the molar ratio of the initiator to the functional monomer is 0.006:1, and the mass ratio of the solvent to the functional monomer is 10:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reactor to generate a polymerization reaction, provided that the polymerization reaction temperature is 120°C, the pressure is 10 MPa, the supply time is 4 hours, and the total residence time is 6 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0147] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is subjected to pressurized argon gas filtration using a 3-in-1 filter. The resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is cyclohexane, the drying temperature is 110°C, the drying time is 24 hours, and the pressure is 1 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0148] Step (3): The liquid phase substance from step (2) is separated by distillation. The top fraction after distillation is returned to steps (1) and (2) respectively as the solvent for each component and reused for preparing the raw material liquid and washing the filtration cake.

[0149] Example I-5 In this embodiment, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0150] Step (1): After introducing a low-carbon olefin into a tubular reactor, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, argon gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, initiator and solvent is pumped into the tubular reactor, provided that the functional monomer is maleic acid, the initiator is azodiisobutyronitrile and lauroyl peroxide in a molar ratio of 1:1, the solvent is xylene, the molar ratio of the initiator to the functional monomer is 0.2:1, and the mass ratio of the solvent to the functional monomer is 40:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reactor to generate a polymerization reaction, provided that the polymerization reaction temperature is 50°C, the pressure is 3 MPa, the supply time is 10 h, and the total residence time is 15 h; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0151] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is filtered using an atmospheric pressure filter, and the resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is xylene, the drying temperature is 120°C, the time is 12 hours, and the pressure is 10 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0152] Step (3): The liquid phase substance from step (2) is separated by distillation. The top fraction after distillation is returned to steps (1) and (2) as a recovered solvent for reuse, and is used for preparing the raw material liquid and washing the filtration cake.

[0153] Example I-6 In this embodiment, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0154] Step (1): After introducing a low-carbon olefin into the reaction vessel, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, initiator and solvent is pumped into the reaction vessel, provided that the functional monomer is maleic anhydride, the initiator is 2,2'-azobis(isobutyrate)dimethyl, the solvent is butyl acetate and ethyl acetate in a volume ratio of 5:1, the molar ratio of the initiator to the functional monomer is 0.008:1, and the mass ratio of the solvent to the functional monomer is 10:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reaction vessel to initiate a polymerization reaction, provided that the polymerization reaction temperature is 110°C, the pressure is 6 MPa, the supply time is 3 hours, and the total residence time is 5 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0155] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is filtered using an atmospheric pressure filter, and the resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is propyl ether, the drying temperature is 50°C, the time is 36 hours, and the pressure is 70 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0156] Step (3): The liquid phase substance from step (2) is separated by rectification. The top fraction after rectification is returned to steps (1) and (2) respectively as the solvent for each component and reused for preparing the raw material liquid and washing the filtration cake.

[0157] Example I-7 In this embodiment, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0158] Step (1): After introducing a low-carbon olefin into the reaction vessel, the temperature and pressure are increased, provided that the low-carbon olefin is propylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, an initiator, and a solvent is pumped into the reaction vessel in a continuous raw material feeding mode, provided that the functional monomer is maleic anhydride, the initiator is azodicyclohexylcarbonitrate, the solvent is n-octane, the molar ratio of the initiator to the functional monomer is 0.15:1, and the mass ratio of the solvent to the functional monomer is 30:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reaction vessel to initiate a polymerization reaction, provided that the polymerization reaction temperature is 60°C, the pressure is 3.5 MPa, the supply time is 7 hours, and the total residence time is 10 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0159] For the operations in steps (2) and (3), please refer to Example 4.

[0160] Based on the measurements of the raw material monomers and olefin functional polymers in Examples I-1 to I-7 described above, the conversion rate of the functional monomers, the yield and anhydrous value of the olefin functional polymers were calculated. Furthermore, the particle size and weight-average molecular weight of the polymers were measured and calculated, and the results are shown in Table 1. [Table 1]

[0161] As is clear from Table 1, when synthesizing olefin functional polymers by the method described in this application, the conversion rate of functional monomers can be increased to over 98% and the polymer yield can be increased to over 93% by adjusting polymerization process parameters such as temperature, pressure, material input ratio, time, and solvent mass ratio. In addition, the anhydride value of the polymer can be increased to over 63.5%, the average particle size can be in the range of 12-22 μm, the particle size range can be controlled to about 10-50 μm, and the weight-average molecular weight can be controlled to about 60,000. During the polymerization process, the higher the temperature, the faster the decomposition of the initiator, resulting in slightly too low a ratio of monomer radicals and initiator radicals in the system, leading to a low degree of polymerization and a low molecular weight of the product; the higher the pressure during the polymerization process, the higher the proportion of monomer radicals and the higher the molecular weight of the product. At the same time, parameters such as the material input ratio of the initiator, the amount of solvent added, and the material supply time have a maximum influence on the polymerization effect.

[0162] The method described herein enables the synthesis of olefin functional polymers of different molecular weights by adjusting process parameters such as temperature, pressure, mixing ratio of raw material liquids, and material supply rate. The following are typical and non-limiting supplementary examples of the synthesis of olefin functional polymers of different molecular weights according to this application.

[0163] Example I-8 In this embodiment, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0164] Step (1): After introducing a low-carbon olefin into a tubular reactor, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, an initiator, and a solvent is pumped into the tubular reactor in a continuous raw material feeding mode, provided that the functional monomer is maleic anhydride, the initiator is azodiisobutyronitrile, the solvent is isoamyl acetate, the molar ratio of the initiator to the functional monomer is 0.02:1, and the mass ratio of the solvent to the functional monomer is 20:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reactor to generate a polymerization reaction, provided that the polymerization reaction temperature is 150°C, the pressure is 1 MPa, the supply time is 4 hours, and the total residence time is 6 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0165] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is filtered using an atmospheric pressure filter, and the resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is n-hexane, the drying temperature is 30°C, the time is 16 hours, and the pressure is 30 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0166] Step (3): The liquid phase substance from step (2) is separated by rectification. The top fraction after rectification is returned to steps (1) and (2) respectively as the solvent for each component and reused for preparing the raw material liquid and washing the filtration cake.

[0167] Example I-9 In this embodiment, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0168] Step (1): After introducing a low-carbon olefin into a tubular reactor, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, an initiator, and a solvent is pumped into the tubular reactor in a continuous raw material feeding mode, provided that the functional monomer is maleic anhydride, the initiator is azodiisobutyronitrile, the solvent is isoamyl acetate, the molar ratio of the initiator to the functional monomer is 0.01:1, and the mass ratio of the solvent to the functional monomer is 10:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reactor to generate a polymerization reaction, provided that the polymerization reaction temperature is 120°C, the pressure is 3 MPa, the supply time is 5 hours, and the total residence time is 8 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0169] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is filtered using an atmospheric pressure filter, and the resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is isoamyl acetate, the drying temperature is 140°C, the drying time is 36 hours, and the pressure is 60 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0170] Step (3): The liquid phase substance from step (2) is separated by distillation. The top fraction after distillation is returned to steps (1) and (2) as a recovered solvent for reuse, and is used for preparing the raw material liquid and washing the filtration cake.

[0171] Example I-10 In this embodiment, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0172] Step (1): After introducing a low-carbon olefin into a tubular reactor, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, an initiator, and a solvent is pumped into the tubular reactor in a continuous raw material feeding mode, provided that the functional monomer is maleic anhydride, the initiator is azodiisobutyronitrile, the solvent is isoamyl acetate, the molar ratio of the initiator to the functional monomer is 0.008:1, and the mass ratio of the solvent to the functional monomer is 3:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reactor to generate a polymerization reaction, provided that the polymerization reaction temperature is 80°C, the pressure is 6 MPa, the supply time is 6 h, and the total residence time is 8 h; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0173] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is filtered using an atmospheric pressure filter, and the resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is xylene, the drying temperature is 100°C, the time is 60 h, and the pressure is 101 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0174] Step (3): The liquid phase substance from step (2) is separated by rectification. The top fraction after rectification is returned to steps (1) and (2) respectively as the solvent for each component and reused for preparing the raw material liquid and washing the filtration cake.

[0175] Example I-11 In this embodiment, a method for synthesizing olefin functional polymers using a continuous raw material feeding mode is proposed, and the method includes the following steps.

[0176] Step (1): After introducing a low-carbon olefin into a tubular reactor, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, an initiator, and a solvent is pumped into the tubular reactor in a continuous raw material feeding mode, provided that the functional monomer is maleic anhydride, the initiator is azodiisobutyronitrile, the solvent is isoamyl acetate, the molar ratio of the initiator to the functional monomer is 0.01:1, and the mass ratio of the solvent to the functional monomer is 5:1; the raw material solution is preheated and then pressurized by a transfer pump before being pumped into the reactor to generate a polymerization reaction, provided that the polymerization reaction temperature is 70°C, the pressure is 4.5 MPa, the supply time is 8 hours, and the total residence time is 10 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0177] Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first, and low-carbon olefins are recovered simultaneously. The discharged low-carbon olefins are pressurized and returned to Step (1) for reuse. The excess material is filtered using an atmospheric pressure filter, and the resulting filtration cake is washed, dried, and then crushed. The solvent used for washing is ethyl ether, the drying temperature is 30°C, the time is 8 hours, and the pressure is 80 kPa. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles.

[0178] Step (3): The liquid phase substance from step (2) is separated by rectification. The top fraction after rectification is returned to steps (1) and (2) respectively as the solvent for each component and reused for preparing the raw material liquid and washing the filtration cake.

[0179] Based on the measurements of the raw material monomers and olefin functional polymers in Examples I-8 to I-11 described above, the conversion rate of the functional monomers, the yield of the olefin functional polymers, and the anhydrous value were calculated. Furthermore, the particle size and weight-average molecular weight of the polymers were measured and calculated, and the results are shown in Table 2. [Table 2]

[0180] As is clear from Table 2, when synthesizing olefin functional polymers by the method described in this application, under the premise that neither the conversion rate of the functional monomer nor the polymer yield is significantly reduced, olefin functional polymers with a weight-average molecular weight of 10,000 to 150,000 can be produced by appropriately adjusting and controlling the process parameters.

[0181] In summary, the method described above achieves the same-chain alternating copolymerization of low-carbon gaseous olefins and functional monomers by pressurized reaction, improves monomer concentration and raw material utilization by heterogeneous phase polymerization, synthesizes olefin functional polymers of different molecular weights by adjusting process parameters, and has high reaction efficiency; in this method, a relatively stable emulsion dispersion can be obtained directly after polymerization is complete, the post-processing process is simple, separation and purification are easy, raw materials can be recycled, and the conversion rate of raw materials and the yield of the product are high; such a method is easy to operate, has mild reaction conditions, saves energy consumption, is low cost, and is environmentally friendly.

[0182] (ii) Use of olefin functional polymers In a part of the embodiment for carrying out the invention of this application, the use of an olefin functional polymer is proposed, and the use includes the following steps.

[0183] Step (1): After introducing the low-carbon olefin into the reactor, the temperature and pressure are increased. Once the reaction temperature and pressure are reached, the raw material solution prepared from the functional monomer, initiator, and solvent is added to the reactor to initiate the polymerization reaction;

[0184] Step (2): The material that underwent the polymerization reaction in Step (1) is first subjected to gas-solid-liquid separation to recover the low-carbon olefin, and after the excess material is discharged, solid-liquid separation is performed again to obtain a solid-phase olefin functional polymer and a liquid-phase substance;

[0185] Step (3): The olefin functional polymer obtained in step (2) is mixed with a matrix resin and a filler to obtain a modified reinforced resin;

[0186] An esterification reaction between the olefin functional polymer and alcohols is carried out in step (2) to obtain an adhesive;

[0187] An anti-scaling agent is obtained by performing an anionization reaction on the olefin functional polymer in step (2); Alternatively, the olefin functional polymer obtained in step (2) is mixed with a coupling agent, a pH adjuster, and water to obtain a glass fiber wetting agent.

[0188] The following are typical and non-limiting embodiments of the present invention.

[0189] Example II-1 In this example, a method for synthesizing olefin functional polymers is proposed, and the method includes the following steps.

[0190] Step (1): After introducing a low-carbon olefin into a tubular reactor, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, initiator and solvent is pumped into the tubular reactor, provided that the functional monomer is maleic anhydride, the initiator is azobisisoheptonitrile, the solvent is n-heptane, the molar ratio of the initiator to the functional monomer is 0.2:1, and the mass ratio of the solvent to the functional monomer is 50:1; a polymerization reaction is initiated, provided that the temperature of the polymerization reaction is 60°C, the pressure is 5 MPa, and the residence time is 10 h; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0191] Step (2): The material from which the polymerization reaction in Step (1) has occurred is first subjected to gas-solid-liquid separation to recover the low-carbon olefin. The discharged low-carbon olefin is pressurized and returned to Step (1) for reuse. After the excess material is discharged in solid-liquid form, it is subjected to pressurized filtration with nitrogen gas. The resulting filtration cake is washed and dried, with n-hexane being the solvent used for washing. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles. The liquid-phase substance is subjected to rectification, and the top fraction after rectification is returned to Step (1) and Step (2) as the solvents for each component to be recovered and reused, and used for preparing the raw material liquid and washing the filtration cake.

[0192] Example II-2 In this example, a method for synthesizing olefin functional polymers is proposed, and the method includes the following steps.

[0193] Step (1): After introducing a low-carbon olefin into a microchannel reactor, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged; once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, initiator and solvent is pumped into the reactor, provided that the functional monomer is maleic anhydride, the initiator is azodiisovaleronitrile, the solvent is ethyl benzoate, the molar ratio of the initiator to the functional monomer is 0.1:1, and the mass ratio of the solvent to the functional monomer is 25:1; a polymerization reaction is initiated, provided that the polymerization reaction temperature is 90°C, the pressure is 10 MPa, and the residence time is 0.01 h; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0194] Step (2): The material from which the polymerization reaction in Step (1) has occurred is first subjected to gas-solid-liquid separation to recover the low-carbon olefin. The discharged low-carbon olefin is pressurized and returned to Step (1) for reuse. After the excess material is discharged in solid-liquid form, it is subjected to pressurized filtration with nitrogen gas. The resulting filtration cake is washed and dried, with n-hexane being the solvent used for washing. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles. The liquid-phase substance is subjected to rectification, and the top fraction after rectification is returned to Step (1) and Step (2) as the solvents for each component to be recovered and reused, and used for preparing the raw material liquid and washing the filtration cake.

[0195] Example II-3 In this example, a method for synthesizing olefin functional polymers is proposed, and the method includes the following steps.

[0196] Step (1): After introducing a low-carbon olefin into the reaction vessel, the temperature and pressure are increased, provided that the low-carbon olefin is ethylene; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, initiator and solvent is pumped into the reaction vessel, provided that the functional monomer is maleic anhydride, the initiator is azobisisoheptonitrile, the solvent is isoamyl acetate, the molar ratio of the initiator to the functional monomer is 0.015:1, and the mass ratio of the solvent to the functional monomer is 10:1; a polymerization reaction is initiated, provided that the polymerization reaction temperature is 110°C, the pressure is 3 MPa, and the residence time is 5 h; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0197] Step (2): The material from which the polymerization reaction in Step (1) has occurred is first subjected to gas-solid-liquid separation to recover the low-carbon olefin, the discharged low-carbon olefin is pressurized and returned to Step (1) for reuse, the excess material is discharged in solid-liquid form, and then pressurized filtration with nitrogen gas is performed, and the resulting filtration cake is dried, thereby obtaining a solid-phase olefin functional polymer and a liquid-phase substance, wherein the olefin functional polymer is in the form of microspherical particles; the liquid-phase substance is subjected to distillation, and the top fraction after distillation is returned to Step (1) for reuse as the solvent for each component recovered and used in the preparation of the raw material liquid.

[0198] Example II-4 In this example, a method for synthesizing olefin functional polymers is proposed, and the method includes the following steps.

[0199] Step (1): After introducing a low-carbon olefin into a tubular reactor, the temperature and pressure are increased, provided that the low-carbon olefin is propylene; before introducing the low-carbon olefin, argon gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, initiator and solvent is pumped into the tubular reactor, provided that the functional monomer is maleimide, the initiator is dicumyl peroxide, the solvent is butyl acetate and xylene in a volume ratio of 1:1, the molar ratio of the initiator to the functional monomer is 0.005:1, and the mass ratio of the solvent to the functional monomer is 6:1; a polymerization reaction is initiated, provided that the polymerization reaction temperature is 120°C, the pressure is 2 MPa, and the residence time is 4 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0200] Step (2): The material from which the polymerization reaction in Step (1) has occurred is first subjected to gas-solid-liquid separation to recover the low-carbon olefin. The discharged low-carbon olefin is pressurized and returned to Step (1) for reuse. After the excess material is discharged in solid-liquid form, it is subjected to pressurized argon gas filtration, and the resulting filtration cake is washed and dried, with n-hexane being the solvent used for washing. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles. The liquid-phase substance is subjected to rectification, and the top fraction after rectification is returned to Step (1) and Step (2) as the solvents for each component to be recovered and reused, and used for preparing the raw material liquid and washing the filtration cake.

[0201] Example II-5 In this example, a method for synthesizing olefin functional polymers is proposed, and the method includes the following steps.

[0202] Step (1): After introducing a low-carbon olefin into a tubular reactor, the temperature and pressure are increased, provided that the low-carbon olefin is 1-butene; before introducing the low-carbon olefin, argon gas is introduced and purged; once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, initiator and solvent is pumped into the tubular reactor, provided that the functional monomer is maleic acid, the initiator is lauroyl peroxide, the solvent is ethyl phenylethyl acetate, the molar ratio of the initiator to the functional monomer is 0.08:1, and the mass ratio of the solvent to the functional monomer is 20:1; a polymerization reaction is initiated, provided that the polymerization reaction temperature is 100°C, the pressure is 7 MPa, and the residence time is 3 hours; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0203] Step (2): The material from which the polymerization reaction in Step (1) has occurred is first subjected to gas-solid-liquid separation to recover the low-carbon olefin. The discharged low-carbon olefin is pressurized and returned to Step (1) for reuse. After the excess material is discharged in solid-liquid form, it is subjected to pressurized argon gas filtration, and the resulting filtration cake is washed and dried, with n-hexane being the solvent used for washing. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles. The liquid-phase substance is subjected to rectification, and the top fraction after rectification is returned to Step (1) and Step (2) as the solvent for each component to be recovered for reuse, and is used for preparing the raw material liquid and washing the filtration cake.

[0204] Example II-6 This example proposes a method for synthesizing a multi-component olefin functional polymer, the method comprising the following steps.

[0205] Step (1): After introducing low-carbon olefin into the reaction vessel, the temperature and pressure are increased, wherein the low-carbon olefin is ethylene and propylene in a molar ratio of 1:1; before introducing the low-carbon olefin, nitrogen gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, initiator, copolymer monomer and solvent is pumped into the reaction vessel, wherein the functional monomer is maleic anhydride, the initiator is dibenzoyl peroxide, the solvent is cyclohexane and ethyl acetate in a volume ratio of 5:1, the copolymer monomer is vinyl acetate, the molar ratio of the initiator to the functional monomer is 0.15:1, the mass ratio of the solvent to the functional monomer is 35:1, and the molar ratio of the copolymer monomer to the functional monomer is 5:1; a polymerization reaction is initiated, wherein the polymerization reaction temperature is 80°C, the pressure is 6 MPa, and the residence time is 8 h; low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0206] Step (2): The material from which the polymerization reaction in Step (1) has occurred is first subjected to gas-solid-liquid separation to recover the low-carbon olefin. The discharged low-carbon olefin is pressurized and returned to Step (1) for reuse. After the excess material is discharged in solid-liquid form, it is subjected to pressurized filtration with nitrogen gas. The resulting filtration cake is washed and dried, however, the solvent used for washing is propyl ether; in this way, a ternary olefin functional polymer and a liquid phase substance are obtained, however, the ternary olefin functional polymer is in the form of microspherical particles; rectification is performed on the liquid phase substance, and the top fraction after rectification is returned to Step (1) and Step (2) respectively as the solvent for each component to be recovered and reused, and used for preparing the raw material liquid and washing the filtration cake.

[0207] Example II-7 In this example, a method for synthesizing olefin functional polymers is proposed, and the method includes the following steps.

[0208] Step (1): After introducing a low-carbon olefin into a fluidized bed reactor, the temperature and pressure are increased, provided that the low-carbon olefin is 1-butene; before introducing the low-carbon olefin, argon gas is introduced and purged, and once the reaction temperature and pressure are reached, a raw material solution prepared from a functional monomer, initiator and solvent is pumped into the fluidized bed reactor, provided that the functional monomer is maleic anhydride, the initiator is 2,2'-azobis(isobutyrate)dimethyl and lauroyl peroxide in a molar ratio of 1:1, the solvent is ethyl acetate, the molar ratio of the initiator to the functional monomer is 0.002:1, and the mass ratio of the solvent to the functional monomer is 3:1; a polymerization reaction is initiated, provided that the polymerization reaction temperature is 150°C, the pressure is 0.5 MPa, and the residence time is 1.5 h; the low-carbon olefin is continuously introduced during the polymerization reaction to maintain the pressure;

[0209] For the operation of step (2), refer to Example 1.

[0210] Based on measurements of the raw material monomer and olefin functional polymer content before and after the reaction in the above examples, the conversion rate of the functional monomer, the yield of the olefin functional polymer, and the anhydride value were calculated. Furthermore, the molecular weight and particle size of the polymer were measured and calculated, and the results are shown in Table 3. [Table 3]

[0211] As is clear from Table 3, in Examples II-1 to II-5 and II-7 above, when olefin functional polymers are synthesized using low-carbon olefins and functional monomers as raw materials by the method described above, the conversion rate of the functional monomers can reach 88% or more, and the polymer yield can reach 95% or more in all cases. In addition, the anhydride value of the polymer is 60% or more, the molecular weight is in the range of 25,000 to 65,000, and the particle size range is 10 to 50 μm. On the other hand, in Example II-6, when copolymer monomers are added as raw materials, the anhydride value of the synthesized multi-component olefin copolymer can be effectively adjusted.

[0212] Application Example 1 In this application example, the olefin functional polymer synthesized in Example II-1 is used as a compatible modifier to produce a modified and reinforced resin, specifically including the following steps.

[0213] An olefin functional polymer is mixed with a matrix resin PA6 and glass fibers as a filler, with the matrix resin accounting for 67.0 wt% of the total mixture, the filler accounting for 28.7 wt% of the total mixture, and the olefin functional polymer accounting for 4.3 wt% of the total mixture. The mixing method is mechanical blending, specifically, the olefin functional polymer is pre-mixed with the matrix resin and filler, and then kneaded and mixed in a kneader at a temperature of 230°C. The glass fiber-reinforced PA6 resin is then produced by extrusion granulation using a twin-screw extruder.

[0214] Application Example 2 In this application example, the olefin functional polymer synthesized in Example II-2 is used as a compatible modifier to produce a modified and reinforced resin, specifically including the following steps.

[0215] An olefin functional polymer is mixed with a matrix resin PET and a filler glass fiber as a compatibility modifier, wherein the amount of matrix resin added accounts for 73.6 wt% of the total mixture, the amount of filler added accounts for 18.4 wt% of the total mixture, and the amount of olefin functional polymer added accounts for 8 wt% of the total mixture. The mixing method is solution blending, specifically, the olefin functional polymer, matrix resin and filler are dissolved in the solvent N-methylpyrrolidone, and after uniform mixing, the solvent is removed, wherein the solvent is removed by distillation; in this way, a PET resin modified and strengthened with glass fiber is obtained.

[0216] Application Example 3 In this application example, the olefin functional polymer synthesized in Example II-1 is used in the manufacture of an adhesive, and specifically includes the following steps.

[0217] An esterification reaction is carried out between an olefin functional polymer and methanol, wherein the molar ratio of acid anhydride in the olefin functional polymer to methanol is 1:3, the temperature of the esterification reaction is 65°C, and the duration is 4 hours; then, the mixture is concentrated and dried to obtain the esterification product, which can be used as an adhesive.

[0218] Application Example 4 In this application example, the olefin functional polymer synthesized in Example II-3 is used in the manufacture of an adhesive, and specifically includes the following steps.

[0219] An esterification reaction is carried out between an olefin functional polymer and ethanol, wherein the molar ratio of acid anhydride in the olefin functional polymer to ethanol is 1:5, the temperature of the esterification reaction is 80°C, and the time is 3h; then, the mixture is concentrated and dried to obtain an esterification product, and the esterification product is further mixed with a thickener, a filler, and water while stirring, wherein the thickener contains diphenylmethane diisocyanate, the filler contains calcium carbonate, the mass ratio of the esterification product, diphenylmethane diisocyanate, calcium carbonate, and water is 10:2:5:40, the stirring speed is 200 r / min, and the stirring time is 10 min; thus, an adhesive is obtained.

[0220] Application Example 5 In this application example, the olefin functional polymer synthesized in Example II-1 is used in the production of a scale inhibitor, and specifically includes the following steps.

[0221] An esterification reaction is carried out between an olefin functional polymer and methanol, where the molar ratio of acid anhydride in the olefin functional polymer to methanol is 1:5, the temperature of the esterification reaction is 65°C, the pressure is 0.13 MPa, and the time is 4 hours; then, condensation and phase separation are performed, and the collected ester-containing fraction is filtered under reduced pressure and dried to obtain monoesterified polyethylene maleic anhydride;

[0222] Furthermore, monoesterified polyethylene maleic anhydride is mixed with epoxypropyltrimethylammonium chloride and dichloromethane as a solvent and reacted, while simultaneously adding an alkaline solution of sodium hydroxide, provided that the molar ratio of carboxyl groups in the monoesterified polyethylene maleic anhydride to epoxypropyltrimethylammonium chloride is 1:1.5, the reaction temperature is 80°C, and the reaction time is 4 hours; after the reaction, the solvent is removed by vacuum distillation, and the excess material is recrystallized in an acetone / ethanol mixed solvent and then vacuum dried to obtain a scale inhibitor for amine salt type cationic polymers.

[0223] Application Example 6 In this application example, the olefin functional polymer synthesized in Example II-4 is used in the production of a scale inhibitor, and specifically includes the following steps.

[0224] After mixing an olefin functional polymer with a sodium hydroxide solution, a saponification reaction is carried out, wherein the molar ratio of acid anhydride to sodium hydroxide in the olefin functional polymer is 1:4, the reaction temperature is 120°C, and the duration is 6 hours; after the reaction, water is removed by vacuum distillation, and the excess material is washed with cyclohexane and then vacuum dried to obtain a carboxylate salt type anionic polymer scale inhibitor.

[0225] Application Example 7 In this application example, the olefin functional polymer synthesized in Example II-5 is used in the production of a scale inhibitor, and specifically includes the following steps.

[0226] An esterification reaction is carried out between an olefin functional polymer and ethylene glycol, where the molar ratio of acid anhydride to ethylene glycol in the olefin functional polymer is 1:2, the temperature of the esterification reaction is 75°C, the pressure is 0.4 MPa, and the time is 4.5 hours; then, condensation and phase separation are performed, and the collected ester-containing fraction is filtered under reduced pressure and dried to obtain monoesterified polyethylene maleic anhydride;

[0227] Furthermore, monoesterified polyethylene maleic anhydride is dissolved in dichloromethane, and then concentrated sulfuric acid is added and the reaction is carried out, provided that the molar ratio of hydroxyl groups in the monoesterified polypropylene maleic anhydride to sulfuric acid is 1:2, the reaction temperature is 80°C, and the duration is 2 hours; after the reaction, sodium hydroxide solution is added to adjust the pH to 7, dichloromethane is removed by vacuum distillation, and the excess material is dried and pulverized to obtain a scale inhibitor for sulfate ester-type anionic polymers.

[0228] Application Example 8 In this application example, the olefin functional polymer synthesized in Example II-5 is used in the production of a glass fiber wetting agent, and specifically includes the following steps.

[0229] The olefin functional polymer is mixed with coupling agent A-151, lubricant stearamide, defoamer polyoxypropylene glyceryl ether, and water, where the mass fraction of water is 95%, and the remaining components, calculated by parts by mass, are 80% ternary olefin functional polymer, 10% coupling agent, 5% lubricant, and 5% defoamer; specifically, the coupling agent is added to the water and stirred for 25 minutes, then the lubricant, ternary olefin functional polymer, and defoamer are added and stirred for 60 minutes, with a stirring speed of 800 rpm; finally, a glass fiber wetting agent is obtained.

[0230] Application Example 9 In this application example, the ternary olefin functional polymer synthesized in Example II-6 is used in the production of a glass fiber wetting agent, specifically including the following steps.

[0231] A ternary olefin functional polymer is mixed with a coupling agent KH-570, ammonia water as a pH adjuster, oleic acid amide as a lubricant, polyoxyethylene polyoxypropylene pentaerythritol ether as an antifoaming agent, antioxidant 1076, and water, where the mass fraction of water is 80%, and the remaining components, calculated by mass parts, are 70% ternary olefin functional polymer, 20% coupling agent, 5% antifoaming agent, 1% antioxidant, and 4% pH adjuster; specifically, the coupling agent is added to water and stirred for 30 minutes, then the lubricant, ternary olefin functional polymer, antifoaming agent, and antioxidant are added and stirred for 80 minutes, with a stirring speed of 600 rpm; after that, the pH adjuster is added to adjust the pH value to 9, and in this way a glass fiber wetting agent is obtained.

[0232] As is clear from the above application examples, the olefin functional polymers synthesized in the examples can be further reacted and used in the production of modified reinforced resins, adhesives, scale inhibitors, and glass fiber wetting agents, enabling applications in various fields, and moreover, the performance of all products meets the standards of the respective types of products.

[0233] In summary, the above examples demonstrate that the present invention achieves the same-chain alternating copolymerization of a low-carbon gaseous olefin and a liquid functional monomer through a pressurized reaction and heterogeneous phase polymerization method, thereby obtaining an olefin functional polymer with a high functional group content, high reaction activity, and wide applicability; by continuously supplying the raw material liquid, the monomer and initiator concentrations during the reaction can be adjusted in real time, increasing the monomer concentration and raw material utilization rate, and allowing for adjustment and control of the molecular weight of the olefin functional polymer; in addition, using the olefin functional polymer as a reaction platform, various modified materials suitable for different fields can be produced through chemical reactions such as esterification, hydrolysis, and modification, enabling the development of various downstream products and expanding the application range of the olefin functional polymer; the present invention offers a simple operation process, mild reaction conditions, easy separation and purification, reusable raw materials, energy savings, low costs, and high economic benefits.

[0234] Although the detailed method of the present application has been illustrated by the above embodiments, the present application is not limited to the detailed method described above, that is, it does not mean that the implementation of the present application must depend on the detailed method described above. It will be obvious to those skilled in the art that any improvements to the present application, equivalent substitutions of the method, addition of auxiliary steps, and selection of specific methods are all within the scope of protection and disclosure of the present application.

Claims

1. A method for synthesizing olefin functional polymers using a continuous raw material feeding mode, Step (1): After introducing low-carbon olefins into the reactor, the temperature and pressure are increased, and once the reaction temperature and pressure are reached, the raw material solution prepared from functional monomers, initiators and solvents is added to the reactor in a continuous raw material feeding mode to initiate the polymerization reaction. Step (2): A method characterized by comprising the steps of first performing gas-solid-liquid separation on the system in which the polymerization reaction in step (1) has occurred to recover the low-carbon olefin, returning the discharged low-carbon olefin to step (1) for reuse, discharging excess material, and then performing solid-liquid separation to obtain a solid-phase olefin functional polymer and a liquid-phase substance.

2. The low-carbon olefin in step (1) comprises one or at least two of ethylene, propylene, butene, and butadiene, Preferably, the method according to claim 1, characterized in that the reactor is evacuated and then replaced with a protective gas before introducing the low-carbon olefin in step (1).

3. The reactor in step (1) includes one of the following: a reaction vessel, a tubular reactor, a microchannel reactor, a fluidized bed reactor, or a boiling bed reactor. Preferably, the tubular reactor includes one of the following: a horizontal tubular reactor, an upright tubular reactor, a coil reactor, or a U-tube reactor. Preferably, the method according to 1 or 2, wherein the microchannel reactor includes a gas-liquid-solid three-phase catalytic microreactor.

4. The functional monomer in step (1) comprises one or at least two of the following: maleic anhydride, maleimide, or maleic acid. Preferably, the initiator in step (1) includes an azo compound and / or a peroxide compound. Preferably, the azo compound comprises one or at least two of the following: azodiisobutyronitrile, azodiisovaleronitrile, azobisisoheptonitrile, azodicyclohexylcarbonite, and 2,2'-azobis(isobutyrate)dimethyl. Preferably, the peroxide compound comprises one or at least two of the following: dibenzoyl peroxide, dicumyl peroxide, diisopropyl peroxydicarbonate, diisobutyryl peroxide, bis(2,4-dichlorobenzoyl) peroxide, dilauroyl peroxide, and t-butylperoxyneoheptanoate. Preferably, the solvent in step (1) comprises one or at least two of the following: an organoalkyl acid ester compound, an alkane compound, or an aromatic hydrocarbon compound. Preferably, the general formula of the organoalkyl acid ester compound is represented by the following formula 1, 【Chemistry 1】 In the formula, R １ R is one of H, C1-C20 alkane groups, or C6-C10 aromatic hydrocarbon groups. ２ It is one of the following: C1-C20 alkanes or C6-C10 aromatic hydrocarbon groups. Preferably, the alkane compound comprises one or at least two of the following: n-hexane, cyclohexane, n-pentane, n-heptane, n-octane, or n-decane. Preferably, the method according to any one of claims 1 to 3, wherein the aromatic hydrocarbon compound comprises one or at least two of benzene, toluene, ethylbenzene, and xylene.

5. The molar ratio of the initiator to the functional monomer in step (1) is (0.001 to 0.2):1, preferably (0.001 to 0.03):

1. Preferably, the mass ratio of the solvent to the functional monomer in step (1) is (2 to 50):1, and preferably (2 to 10):

1. Preferably, impurities are removed and preheating is performed before adding the raw material liquid in step (1) to the reactor. Preferably, the method according to any one of claims 1 to 4, characterized in that the raw material liquid in step (1) is pressurized by a transport pump and then pumped into the reactor at a constant rate.

6. The temperature of the polymerization reaction in step (1) is 50°C to 150°C, preferably 70°C to 120°C. Preferably, the pressure of the polymerization reaction in step (1) is 0.1 MPa to 10 MPa, preferably 2 MPa to 8 MPa. Preferably, the supply time of the raw material liquid in step (1) is 0.1h to 10h. Preferably, the residence time of the raw material liquid during step (1) is 0.1h to 15h. Preferably, the method according to any one of claims 1 to 5, characterized in that a low-carbon olefin is continuously introduced and the pressure maintained during the polymerization reaction in step (1).

7. During the gas-solid-liquid separation process in step (2), the low-carbon olefin is discharged and recovered, and replaced with a protective gas. Preferably, the excess material from which the low-carbon olefin has been recovered in step (2) is discharged in solid-liquid form. Preferably, the method according to any one of claims 1 to 6, characterized in that the discharged low-carbon olefin is pressurized and then returned to step (1) for reuse.

8. The method for solid-liquid separation in step (2) includes one or at least two of the following: decantation, filtration, and centrifugation. Preferably, the filtration includes one of gravity filtration, vacuum filtration, or pressure filtration. Preferably, the excess material is subjected to pressure filtration with a protective gas, the resulting filtration cake is washed, dried, and then crushed. Preferably, the washing is carried out using the solvent in step (1), Preferably, the solvent used for the washing further comprises an ether compound, the ether compound comprising any one or at least two combinations of C1 to C10 saturated ether compounds, and preferably ethyl ether and / or propyl ether. Preferably, the drying temperature is 30°C to 150°C, the drying time is 1 hour to 72 hours, and the pressure is 0.1 kPa to 101 kPa. Preferably, the olefin functional polymer in step (2) is a microspherical particle with a particle size of 10 μm to 50 μm, characterized in that the method according to any one of claims 1 to 7.

9. The recovered solvent obtained by separating the liquid phase substance in step (2) is returned to step (1) for reuse. Preferably, the method for separating the liquid phase substance includes one or at least two of the following: distillation, membrane separation, washing, and extraction, and preferably distillation. Preferably, the method according to any one of claims 1 to 8, characterized in that the recovered solvent is returned to step (1) and / or step (2) for reuse and used for preparing the raw material liquid and / or washing the filtration cake.

10. The above method includes the following steps: Step (1): After introducing a low-carbon olefin into the reactor, the temperature and pressure are increased, wherein the low-carbon olefin includes one or at least two of ethylene, propylene, butene, and butadiene, and the reactor includes one of a reaction vessel, a tubular reactor, a microchannel reactor, a fluidized bed reactor, or a boiling bed reactor; once the reaction temperature and pressure are reached, a feedstock solution prepared from a functional monomer, an initiator, and a solvent is added to the reactor in a continuous feedstock mode, wherein the functional monomer includes one or at least two of maleic anhydride, maleimide, or maleic acid, and the initiator is an azo compound and / or a peroxide compound The solvent contains a compound, the solvent comprises one or at least two compounds selected from organic alkyl ester compounds, alkane compounds, or aromatic hydrocarbon compounds, the molar ratio of the initiator to the functional monomer is (0.001 to 0.2):1, and the mass ratio of the solvent to the functional monomer is (2 to 50):1; the raw material liquid is pressurized by a transfer pump and then pumped into the reactor at a constant rate to generate a polymerization reaction, wherein the polymerization reaction temperature is 50°C to 150°C, the pressure is 0.1 MPa to 10 MPa, the supply time is 0.1 h to 10 h, and the residence time is 0.1 h to 15 h; low-carbon olefins are continuously introduced during the polymerization reaction to maintain the pressure; Step (2): In the system where the polymerization reaction in Step (1) has occurred, gas-solid-liquid separation is performed first. During the gas-solid-liquid separation process, excess low-carbon olefin is discharged and replaced with a protective gas. The discharged low-carbon olefin is pressurized and returned to Step (1) for reuse. The excess material is discharged in solid-liquid form and subjected to solid-liquid separation. The excess material is pressure-filtered with a protective gas, and the resulting filtration cake is washed, dried, and then crushed. In this way, a solid-phase olefin functional polymer and a liquid-phase substance are obtained, provided that the olefin functional polymer consists of microspherical particles with a particle size of 10 μm to 50 μm. The method according to any one of claims 1 to 9, characterized in that: step (3): separation is performed on the liquid phase substance obtained in step (2), wherein the separation method includes one or at least two combinations of distillation, membrane separation, washing, and extraction; the recovered solvent obtained is returned to step (1) and / or step (2) for reuse and used for preparing the raw material liquid and washing the filtration cake.

11. The use of olefin functional polymers, The olefin functional polymer is obtained by the method described in any one of claims 1 to 10. The olefin functional polymer is mixed with a matrix resin and a filler to obtain a modified and reinforced resin, preferably the olefin functional polymer is mixed with the matrix resin and filler as a compatibility modifier. Preferably, the matrix resin includes thermoplastics and / or thermosetting plastics. Preferably, the thermoplastic includes one or at least two of the following: PC, PA, POM, PBT, PET, PVC, PS, PE, or ABS. Preferably, the thermosetting plastic comprises one or at least two of EP, UPR, PU, ​​or UF. Preferably, the filler includes inorganic fillers and / or organic fillers. Preferably, the amount of the matrix resin added accounts for 30 wt% to 90 wt% of the total amount of the mixture, the amount of the filler added accounts for 5 wt% to 65 wt% of the total amount of the mixture, and the amount of the olefin functional polymer added accounts for 3 wt% to 15 wt% of the total amount of the mixture. Preferably, the use of an olefin functional polymer is characterized in that the mixing method comprises one of a mechanical blend, a solution blend, or a latex blend.

12. The use of olefin functional polymers, The olefin functional polymer is obtained by the method described in any one of claims 1 to 10. An esterification reaction is carried out between the olefin functional polymer and alcohols to obtain an adhesive. Preferably, the alcohols include one or at least two of methanol, ethanol, propanol, or butanol. Preferably, the molar ratio of acid anhydride to alcohols in the olefin functional polymer is 1:(2-5), Preferably, the temperature of the esterification reaction is 60°C to 80°C. Preferably, the duration of the esterification reaction is 3 to 5 hours. Preferably, the use of an olefin functional polymer is characterized by obtaining an esterification product by concentrating and drying after the esterification reaction.

13. The use of olefin functional polymers, The olefin functional polymer is obtained by the method described in any one of claims 1 to 10. A scale inhibitor is obtained by performing an anionization reaction on the aforementioned olefin functional polymer. Preferably, prior to the anionization reaction, the method further includes generating a monoesterified olefin functional polymer by causing an esterification reaction between the olefin functional polymer and alcohols, Preferably, the alcohols include one or at least two of methanol, ethanol, butanol, ethylene glycol, or propylene glycol. Preferably, the anionization reaction includes the reaction of an olefin functional polymer or a monoesterified olefin functional polymer with a quaternary ammonium salt, an alkali, or an acid. Preferably, the quaternary ammonium salt comprises one or at least two of the following: epoxypropyltrimethylammonium chloride, octadecyldimethylammonium chloride, octadecylamine polyoxyethylene ether bisquaternary ammonium salt, or bisdodecylamine polyoxyethylene ether monoquaternary ammonium salt. Preferably, the alkali includes a caustic alkali added in the form of an alkaline solution. Preferably, the acid comprises one or at least two of the following: sulfuric acid, persulfuric acid, or phosphorus pentoxide. Preferably, the use of an olefin functional polymer is characterized in that the anionization reaction includes one or at least two of the following: reacting a monoesterified olefin functional polymer with a quaternary ammonium salt in an alkaline solution to produce a cationic polymer scale inhibitor; reacting an olefin functional polymer with a quaternary ammonium salt in an alkaline solution to produce a cationic polymer scale inhibitor; generating a saponification reaction between an olefin functional polymer and an alkaline solution to produce a carboxylate type anionic polymer scale inhibitor; reacting a diol-based monoesterified olefin functional polymer with sulfuric acid to produce a sulfate ester type anionic polymer scale inhibitor; or reacting a diol-based monoesterified olefin functional polymer with phosphorus pentoxide to produce a phosphate type anionic polymer scale inhibitor.

14. The use of olefin functional polymers, The olefin functional polymer is obtained by the method described in any one of claims 1 to 10. The olefin functional polymer is mixed with a coupling agent, a pH adjuster, and water to obtain a glass fiber wetting agent. Preferably, the coupling agent comprises one or at least two of the following: a silane coupling agent, an aluminate ester coupling agent, or a titanate ester coupling agent. The pH adjusting agent includes an acid adjusting agent or an alkali adjusting agent. Preferably, the acidity adjusting agent comprises one or at least two of acetic acid, citric acid, formic acid, or oxalic acid. Preferably, the alkalinity adjusting agent comprises one or at least two of the following: aqueous ammonia, sodium hydroxide, sodium bicarbonate, alkaline amino acids, or organic amine systems. Preferably, the manufacturing process of the glass fiber wetting agent includes adding a coupling agent to water and stirring, then adding an olefin functional polymer, stirring uniformly, and then adding a pH adjusting agent to obtain the glass fiber wetting agent in this way. Preferably, after adding the coupling agent, the stirring time is 20 min to 30 min. Preferably, after adding the olefin functional polymer, the stirring time is 60 min to 240 min, and the stirring speed is 100 rpm to 800 rpm. Preferably, after adding a pH adjusting agent, the pH value is adjusted to 6 to 10. Preferably, in the glass fiber wetting agent, the mass percentage of water is 20 wt% to 95 wt%, and the remainder is a solid phase component. Preferably, the glass fiber wetting agent further comprises one or at least two of the following: a lubricant, an antifoaming agent, or an antioxidant. Preferably, the use of an olefin functional polymer is characterized in that the lubricant, defoamer, and antioxidant are added simultaneously with the multi-component olefin functional polymer during the production of the glass fiber wetting agent.

15. The use of olefin functional polymers, The olefin functional polymer is obtained by the method described in any one of claims 1 to 10. Step (1): After introducing a low-carbon olefin into the reactor, the temperature and pressure are increased, wherein the low-carbon olefin includes one or at least two of ethylene, propylene, butene, or butadiene, and the reactor includes one of a kettle reactor, a tubular reactor, a microchannel reactor, a column reactor, a fluidized bed reactor, or a boiling bed reactor; once the reaction temperature and pressure are reached, a feedstock solution prepared from a functional monomer, an initiator, and a solvent is added to the reactor, wherein the functional monomer includes one or at least two of maleic anhydride, maleimide, or maleic acid, and the initiator is an azo compound and / or The material comprises a peroxide compound, the solvent comprises one or at least two combinations of an organic alkyl ester compound, an alkane compound, or an aromatic hydrocarbon compound, the molar ratio of the initiator to the functional monomer is (0.001 to 0.2):1, and the mass ratio of the solvent to the functional monomer is (2 to 50):1; the raw material liquid is pressurized by a transfer pump and then pumped into the reactor at a constant rate to generate a polymerization reaction, wherein the temperature of the polymerization reaction is 50°C to 150°C, the pressure is 0.1 MPa to 10 MPa, and the residence time is 10 s to 10 h; the process includes a step of continuously introducing a low-carbon olefin during the polymerization reaction to maintain the pressure, Step (2): The substance from which the polymerization reaction in Step (1) has occurred is first subjected to gas-solid-liquid separation to recover the low-carbon olefin, the discharged low-carbon olefin is pressurized and returned to Step (1) for reuse, the excess material is discharged in solid-liquid form and subjected to solid-liquid separation, pressurized filtration with a protective gas is performed, the resulting filtration cake is washed and dried, and in this way a solid-phase olefin functional polymer and a liquid-phase substance are obtained, wherein the olefin functional polymer is in the form of microspherical particles with a particle size of 10 μm to 50 μm; separation is performed on the liquid-phase substance, wherein the separation method includes one or at least two combinations of distillation, membrane separation, washing, or extraction; the separated recovered solvent is returned to Step (1) and / or Step (2) for reuse and used for preparing the raw material liquid and washing the filtration cake. Step (3): Mix the olefin functional polymer obtained in Step (2) with a matrix resin and a filler as a compatible modifier, wherein the matrix resin includes thermoplastics and / or thermosetting plastics, the filler includes inorganic fillers and / or organic fillers, the amount of the matrix resin added accounts for 30 wt% to 90 wt% of the total amount of the mixture, the amount of the filler added accounts for 5 wt% to 65 wt% of the total amount of the mixture, and the amount of the olefin functional polymer added accounts for 3 wt% to 15 wt% of the total amount of the mixture, and the mixing method includes one of mechanical blending, solution blending or latex blending; thus obtaining a modified and strengthened resin, Step (2) is used to induce an esterification reaction between the olefin functional polymer and alcohols, wherein the alcohols include one or at least two of methanol, ethanol, propanol, or butanol, the molar ratio of acid anhydride to alcohols in the olefin functional polymer is 1:(2-5), the temperature of the esterification reaction is 60°C to 80°C, the time is 3h to 5h, and further concentration and drying are performed to obtain the adhesive; Step (2) involves performing an anionization reaction on the olefin functional polymer to obtain a scale inhibitor; further comprising, prior to the anionization reaction, generating a monoesterified olefin functional polymer by causing an esterification reaction between the olefin functional polymer and alcohols, wherein the alcohols include one or at least two of methanol, ethanol, butanol, ethylene glycol, or propylene glycol; and the anionization reaction includes the reaction of the olefin functional polymer or monoesterified olefin functional polymer with a quaternary ammonium salt, alkali, or acid, wherein the quaternary ammonium salt is epoxypropyltrimethylammonium chloride, octadecyldimethylammonium chloride, octadecylamine polyoxyethylene ether bisquaternary ammonium salt, or bisdodecylamine polyoxyethylene ether monoquaternary ammonium The anionization reaction includes one or at least two combinations of any nium salts; the anionization reaction includes one or at least two combinations of any of the following: reacting a monoesterified olefin functional polymer with a quaternary ammonium salt in an alkaline solution to produce a cationic polymer scale inhibitor; reacting an olefin functional polymer with a quaternary ammonium salt in an alkaline solution to produce a cationic polymer scale inhibitor; causing a saponification reaction between an olefin functional polymer and an alkaline solution to produce a carboxylate type anionic polymer scale inhibitor; reacting a diol-based monoesterified olefin functional polymer with sulfuric acid to produce a sulfate ester type anionic polymer scale inhibitor; or reacting a diol-based monoesterified olefin functional polymer with phosphorus pentoxide to produce a phosphate type anionic polymer scale inhibitor; Alternatively, the olefin functional polymer prepared in step (2) is mixed with a coupling agent, a pH adjuster, and water. Specifically, the coupling agent is added to the water and stirred for 20 min to 30 min, then a lubricant, the olefin functional polymer, an antifoaming agent, and an antioxidant are added and stirred for 60 min to 240 min, with a stirring speed of 100 rpm to 800 rpm; after which the pH adjuster is added to adjust the pH value to 6 to 10, thereby obtaining a glass fiber wetting agent; however, the coupling agent comprises one or at least two of the following: a silane coupling agent, an aluminate ester coupling agent, or a titanate ester coupling agent; the pH adjuster comprises an acid adjuster or an alkali adjuster; and in the glass fiber wetting agent, the mass percentage of water is 20 wt% to 95 wt%, with the remainder being a solid phase component.

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